Process for the recovery of furfural

ABSTRACT

Disclosed is a process for the extraction of furfural which includes: (a) subjecting a composition comprising furfural, water, at least one acid and an aromatic solvent, with a boiling point higher than that of furfural, to a first separation step providing: (i) an organic phase, and (ii) an aqueous phase; (b) subjecting the aqueous phase of step (a) to a first distillation step to provide: (i) a first in top stream comprising a furfural-water azeotrope; (c) subjecting the first top stream of step (b) to a second separation step to provide: (i) a second top stream comprising a portion of the furfural-water azeotrope; (d) subjecting the second top stream of step (c) to a second distillation step to provide: (i) a third top stream enriched with the furfural-water azeotropic mixture; (e) subjecting the organic phase of step (a) to a third distillation step to provide: a fourth top stream comprising furfural.

CROSS REFERENCE TO RELATED APPLICATIONS

This is a national stage application of International Application No. PCT/US2017/058939, filed 30 Oct. 2017, which claims benefit of priority to U.S. Provisional Patent Application No. 62/415,530, filed 1 Nov. 2016.

FIELD OF THE INVENTION

The present invention relates to a process for the high recovery/extraction of furfural from a composition in an energy efficient manner.

BACKGROUND OF THE INVENTION

Furfural is a useful precursor for industrial chemicals, in particular to produce furan and its derivatives.

Furfural may be produced from the hydrolysis of feedstock comprising lignocellulosic biomass. Lignocellulosic biomass comprises mainly hemicelluloses and cellulose, and smaller portions of lignin and protein. Hemicelluloses are a branched polysaccharide of heterogeneous monosaccharide content. Their molecular structure includes the five-carbon monosaccharides (‘pentose(s)’) xylose and arabinose, as well as the six-carbon monosaccharides (‘hexose(s)’) mannose, galactose and rhamnose. Due to their xylose and arabinose content, hemicelluloses are a suitable source of monomeric and polymeric pentoses. In comparison, cellulose is a linear-polysaccharide made up of polymerised glucose (a six-carbon monosaccharide/hexose). Compared to cellulose, hemicelluloses are easier to breakdown into their constituent monosaccharides.

Commercially available feedstock comprising lignocellulosic biomass includes bagasse, which is the fibrous matter that remains after sugarcane or sorghum stalks are crushed their juices extracted. An established continuous process for the production of furfural from bagasse is the Rosenlew process, the details of which are discussed in “The Chemistry and Technology of Furfural and its Many By-Products”, 1st Edition, K. Zeitsch, pages 48-51 and 303-306.

WO2012041990 describes the production of furfural from bagasse-derived hemicellulose, via its gaseous acid catalysed hydrolysis to pentoses, which are then dehydrated to produce furfural.

WO2016025678 describes the production of furfural, where initially hemicellulose is hydrolysed in a solution comprising α-hydroxysulfonic acid, a portion of the α-hydroxysulfonic acid is then removed from the hydrolysis reaction product to produce an acid-removed stream, and finally the acid-removed stream is subjected to a dehydrating step to produce furfural.

WO2016025679 describes a hydrolysis step, which is buffered to, preferably, less than pH 1, followed by a dehydrating step to produce furfural.

In both WO2016025678 and WO2016025679, during the dehydration reaction step, a “bi-phasic” dehydration reaction mixture is formed by the addition of ‘a water-immiscible organic phase’ (i.e. a solvent) into the dehydration reaction mixture. The dehydration reaction mixture is then separated into an aqueous product stream, and an organic product stream comprising a portion of furfural. However, WO2016025678 and WO2016025679 do not disclose how furfural can be fully recovered and purified from the organic product stream comprising furfural. Further, WO2016025678 and WO2016025679 do not disclose how furfural remaining in the aqueous product stream can be efficiently recovered and purified from the aqueous product stream.

Solvent extraction of furfural from an aqueous environment is complicated by the carry-over of water into the organic phase, as well as the formation of a furfural-water azeotrope. The extent of the water carry-over depends on the solvent used. Oxygenate solvents, such as those of phenolic compounds, carry more water into the organic phase (approximately around 10,000 ppm to around 40,000 ppm), as compared to aromatic solvents (approximately around 200 ppm to around 1,000 ppm). Further, if furfural is present in an aqueous environment, a furfural-water azeotrope can be formed. It is known in the art of extracting chemical compounds from mixtures of compounds that the presence of any azeotrope increases the energy consumption of a given process, as well as complicating the step and the equipment needed for that process. As aromatic solvents have a lesser tendency to carry-over water, on the face of it the furfural-water azeotrope problem should be less severe; however, due to furfural's properties, aromatic solvents' ability to extract furfural is lower, which potentially decreases the overall furfural recovery.

In the Rosenlew process, furfural is isolated from the reaction mix by azeotropic distillation, and no solvent extraction is used. The Rosenlew process consumes about 10 tonnes of steam to recover each tonne of furfural.

It would, therefore, be advantageous to provide a process for the recovery of furfural that is more energy-efficient than the prior art processes, as well as one which provides a high-yield of furfural.

SUMMARY OF THE INVENTION

The present invention provides a process for the extraction of furfural from a composition comprising furfural, water, at least one acid and an aromatic solvent with a boiling point higher than that of furfural; said process comprising:

(a) subjecting the composition to a first liquid-liquid separation step to provide: (i) an organic phase comprising the aromatic solvent and a portion of the furfural, and (ii) an aqueous phase comprising the remainder of the furfural and the at least one acid; (b) subjecting the aqueous phase of step (a) to a first distillation step to provide: (i) a first top stream comprising a furfural-water azeotrope, and (ii) an aqueous waste stream comprising water and the at least one acid; (c) subjecting the first top stream of step (b) to a second liquid-liquid separation step to provide: (i) a second top stream comprising a portion of the furfural-water azeotrope, and (ii) a second bottom stream comprising the remainder of the furfural-water azeotrope; (d) subjecting the second top stream of step (c) to a second distillation step to provide: (i) a third top stream enriched with the furfural-water azeotropic mixture, and (ii) a third bottom stream comprising furfural; (e) subjecting the organic phase of step (a) to a third distillation step to provide: a fourth bottom stream comprising the aromatic solvent, and a fourth top stream comprising furfural.

The composition may be derived from a product stream of a pentose dehydration step wherein a pentose feed stream is dehydrated. The pentose feed stream may be derived from the hydrolysis of a lignocellulosic biomass.

The second bottom stream of step (c) comprising a portion of the furfural-water azeotrope may be subjected to a fourth distillation step to provide: (i) a fifth top stream comprising the furfural-water azeotrope, which is recycled back to feed the second liquid-liquid separation step of step (c), and (ii) a fifth bottom stream comprising water.

The aromatic solvent may be selected from the group consisting of 1-ethyl-2,3-dimethylbenzene, 1-ethyl-2,5-dimethylbenzene, 1-ethyl-2,4-dimethylbenzene, 1-ethyl-3,4-dimethylbenzene, 1,2,3,5-tetramethylbenzene, 1,2,3,4-tetramethylbenzene, 1,2,4,5-tetramethylbenzene, naphthalene, 1-methylnaphthalene, 2-methylnaphthalene, n- and sec-propyl-methyl benzenes (with the methyl group located in 2-,3-,4- or 5-position) n- and sec-butyl benzene and n- and sec-pentyl benzene, or any combination thereof.

The aromatic solvent may have a ratio of aromatic carbons to aliphatic carbons of greater than 1.

The second liquid-liquid separation step may be operated at a temperature range of from ambient temperature to 120° C.

The distillation step may be an atmospheric distillation step or a vacuum distillation step.

The second bottom stream comprising the remainder of the furfural-water azeotrope provided by the second liquid-liquid separation step (c) may be recycled back to feed either the first distillation step of step (b), or the first liquid-liquid separation step of step (a).

The third top stream of step (d) may be recycled back to feed either: (i) the second liquid-liquid separation step of step (c) above, or (ii) the first distillation step of step (b), or (iii) the first liquid-liquid separation step of step (a).

The fourth bottom stream provided by the third distillation step (e) comprising the aromatic solvent may be recycled into the composition.

The aqueous phase provided by the first liquid-liquid separation step (a) may be recycled to feed is recycled to the pentose dehydration step.

BRIEF DESCRIPTION OF THE DRAWING

FIG. 1 shows a simplified schematic diagram of an embodiment of the process according to the invention.

DETAILED DESCRIPTION OF THE INVENTION

The present inventors have surprisingly found that the process for the extraction of furfural according to the present invention provides a higher yield of furfural than known processes, and consumes less energy to produce each tonne of furfural, suitably, by consuming less than 8 tonnes of steam to recover each tonne furfural with a furfural recovery of over 95%.

In the process according to the present invention, furfural is extracted from a composition comprising furfural, water, at least one acid and an aromatic solvent with a boiling point higher than that of furfural.

In an embodiment of the present invention the composition may be derived from a product stream of a pentose dehydration step, wherein a pentose feed stream is dehydrated.

Suitably, the pentose dehydration step dehydrates a pentose feed stream comprising monomeric and polymeric pentoses, which is derived from a hydrolysis step wherein a lignocellulosic biomass is hydrolysed in the presence of at least one inorganic acid; although as an alternative, other processes may also be used to hydrolyse the lignocellulosic biomass, such as ones which may use basic or neutral pH conditions. Suitably, the lignocellulosic biomass hydrolysis step is as described in WO2016025678 and WO2016025679.

Where used for the hydrolysis of lignocellulosic biomass, suitably, the at least one inorganic acid may be selected from, such as but not limited to, hydrochloric acid, nitric acid, phosphoric acid, boric acid sulphuric acid and α-hydroxysulfonic acid, or combinations thereof.

Suitably, some types of lignocellulosic biomass may intrinsically contain at least one organic acid, or will form at least one organic acid upon being subjected to the hydrolysis. Examples of such acids include, but are not limited to, formic acid, acetic acid, lactic acid, glycolic acid, levulinic acid, oxalic acid and citric acid, or combinations thereof. When using such types of biomass material, the need to add at least one acid inorganic acid may be reduced or even eliminated as the in-situ generated acid may provide the necessary acidic pH.

According to an embodiment of the invention, the composition may be derived from the product stream of a pentose dehydration step; said product stream is also hereinafter referred to as the “dehydration product stream”.

Suitably, the pentose dehydration step takes place in a dehydration reaction mixture, where the dehydration of monomeric and polymeric pentoses is catalysed by at least one inorganic acid at an elevated temperature, although at least one organic acid may also take part in such catalysis.

The dehydration reaction mixture comprises the pentose feed stream, at least one inorganic acid, at least one organic acid and furfural; the level of the furfural depending on how long the pentose dehydration step has been running.

The at least one inorganic acid and the at least one organic acid present in the dehydration reaction mixture will have carried through in the pentose feed stream from the hydrolysis step to the pentose dehydration step, where the hydrolysis step precedes the pentose dehydration step. However, if the hydrolysis step was carried out under basic or neutral pH conditions as an alternative, or if it is determined that the pH of the dehydration reaction mixture is not acidic enough, more inorganic acid may be added to the dehydration reaction mixture.

Preferably, the pentose dehydration step is carried out at the elevated temperature of at least 100° C., more preferably at least 110° C., and even more preferably at least 140° C. Preferably, the pentose dehydration step is carried out at the elevated temperature of at most 250° C., more preferably at most 200° C., and even more preferably at most 150° C.

Preferably, the pentose dehydration step is carried out for a period of at least 1 second, more preferably at least 5 minutes, even more preferably at least 10 minutes and most preferably at least 30 minutes. Preferably, the pentose dehydration step is carried out for a period of at most 24 hours, more preferably at most 12 hours, even more preferably at most 5 hours and most preferably at most 2 hours.

One or more aromatic solvents may be added to the dehydration reaction mixture. The presence of the aromatic solvent in the dehydration reaction mixture creates an aqueous phase and an organic phase.

Preferably, the dehydration reaction mixture to aromatic solvent ratio is at least 1 to 0.05% vol., more preferably said ratio is 1 to 0.1% vol., even more preferably said ratio is 1 to 0.25% vol., most preferably said ratio is 1 to 0.4% vol.

Preferably, the dehydration reaction mixture to aromatic solvent ratio is at most 1 to 2.5% vol., more preferably said ratio is 1 to 1.25% vol., even more preferably said ratio is 1 to 0.75% vol., most preferably said ratio is 1 to 0.6% vol.

Preferably, the aromatic solvent is selected from alkyl benzene compounds of 10 or more carbons, alkyl naphthalene compounds of 10 or more carbons, and from naphthalene.

Preferably, the aromatic solvent is selected from compounds such as, but not limited to, 1-ethyl-2,3-dimethylbenzene, 1-ethyl-2,5-dimethylbenzene, 1-ethyl-2,4-dimethylbenzene, 1-ethyl-3,4-dimethylbenzene, 1,2,3,5-tetramethylbenzene, 1,2,3,4-tetramethylbenzene, 1,2,4,5-tetramethylbenzene, naphthalene, 1-methylnaphthalene, 2-methylnaphthalene, n- and sec-propyl-methyl benzenes (with the methyl group located in 2,3,4 or 5 position) n- and sec-butyl benzene and n- and sec-pentyl benzene. Suitably, the aromatic solvent may be a mixture of one or more of such compounds.

Preferably, the aromatic solvent has a ratio of aromatic carbons to aliphatic carbons of greater than 1. If the aromatic solvent is a pure compound, the ratio of aromatic carbons to aliphatic carbons will be evident to the skilled person. However, if the aromatic solvent is a mixture of one or more of such compounds, a method of determining the ratio of aromatic carbons to aliphatic carbons may be by subjecting the aromatic solvent mixture to ¹³C NMR analysis and obtaining a ratio of the peaks representing the aromatic and aliphatic moieties by techniques known in the art.

The aromatic solvent may be added to the dehydration reaction mixture at the start of, or part way through, the pentose dehydration step. Suitably, the aromatic solvent may also be added to the dehydration product stream to form the composition, if the pentose dehydration step did not occur in the presence of the aromatic solvent. However, preferably, the aromatic solvent may be added to the dehydration reaction mixture at the start of the pentose dehydration step. Optionally, the source of the aromatic solvent may be a recycle stream from one or more of steps of the process of the present invention, such stream being recycled as a feed to the pentose dehydration step. If the aromatic solvent is added to the dehydration reaction mixture at the start of, or part way through, the pentose dehydration step, the formation of furfural takes place in the aqueous phase.

Suitably, the aromatic solvent has selectivity towards furfural over water and over the at least one inorganic acid, and selectively extracts furfural from said aqueous phase into the organic phase as the pentose dehydration step converts the pentose feed stream into furfural. The aromatic solvent also has selectivity towards furfural over the at least one organic acid, however a small amount of at least one organic acid may partition into the organic phase depending on how much water any given aromatic solvent may carry over; such small amount is deemed to have insignificant consequence in the process of the present invention.

Therefore the amount of furfural in the organic phase varies depending on how far the pentose dehydration step has progressed.

Suitably, the aromatic solvent provides at least three advantages. Firstly, compared to, for example, oxygenate solvents, the aromatic solvent carries-over less water into the organic phase, and therefore suitably the aromatic solvent does not extract any of the at least one organic acid and any significant amount of at least one inorganic acid into the organic phase. This has the advantage that by selectively extracting the furfural into the organic phase, furfural is removed from the presence of such acids, and therefore any undesired loss of furfural via degradation and/or oligomerisation reactions that may be taking place during the pentose dehydration step are prevented, and therefore furfural yield is improved.

Secondly, again due to the aromatic solvent carrying less water into the organic phase, no furfural-water azeotrope can be formed in the organic phase, which simplifies the separation of furfural from the organic phase of the pentose dehydration step.

Thirdly, because the boiling point of water at ambient pressure is lower than the boiling point of furfural at ambient pressure (about 100° C. versus about 161° C., respectively) extraction of the furfural from the dehydration reaction product stream reduces the need to boil-off significant amount of water to purify the furfural from water. Instead, because the aromatic solvent has a boiling point higher than that of furfural, furfural can be distilled off from the aromatic solvent, and since the quantity of furfural in the aromatic solvent is only a fraction per unit volume of the aromatic solvent, in processes such as distillation, a lesser quantity of material (i.e. the furfural with its lower boiling point) needs to be boiled off. Suitably, this provides an energy advantage (saving).

FIG. 1 shows a simplified schematic diagram of an embodiment of the process according to the invention.

In the process according to the present invention, furfural is extracted from a composition (1) comprising furfural, water, at least one acid, and an aromatic solvent with a boiling point higher than that of furfural.

To commence the extraction of furfural from the composition, the composition (1) is subjected to a first liquid-liquid separation step in a first liquid-liquid separator (14) to provide: (i) a an organic phase (7) comprising the aromatic solvent and a portion of the furfural, and (ii) an aqueous phase (8) comprising the remainder of the furfural and the at least one acid.

Preferably, the first liquid-liquid separation may be operated at a temperature of at most 200° C., more preferably at a temperature of at most 180° C., even more preferably at a temperature of at most 160° C., even more preferably at a temperature of at most 150° C., so long as the liquid separates into two phases at the separation temperature.

Preferably, the first liquid-liquid separation may be operated at a temperature of at least ambient temperature, more preferably at a temperature of at least 60° C., even more preferably at a temperature of at least 100° C., even more preferably at a temperature of at least 130° C., so long as the liquid separates into two phases at the separation temperature.

The first liquid-liquid separation step is carried out in any suitable liquid-liquid separator as would be known to the person skilled in the art.

Prior to undergoing the first liquid-liquid separation step, the composition may optionally be routed through a, preferably solid/liquid, separation step, to remove any insoluble humins or other tar that may have been formed during the dehydration step, and which may otherwise negatively interfere with the separation of the organic phase from the aqueous phase, or the later separation or purification steps. Formation of humins and/or tar is a well-known problem associated with the production of bio-based products. Humins are dark, amorphous and undesirable acid by-products and resinous material resulting from sugars, and other organic compound degradation. Tar is a generic reference to organic material which is insoluble in water, which is dark in colour, and which tends to become viscous and very dark to almost black when concentrated.

In the process of the present invention, the organic phase (7) provided by the first liquid-liquid separation step is subjected to a third distillation step (19) to provide: (i) a fourth bottom stream (3) comprising the aromatic solvent, and (ii) a fourth top stream (2) comprising furfural.

Furfural has a boiling point at ambient pressure of about 161° C., and as the aromatic solvent has a boiling point higher than that of furfural, a top stream comprising furfural is obtained. Suitably, the greater the difference between the boiling point of furfural and the aromatic solvent, the easier and cleaner the separation between these compounds will be.

Suitably the aromatic solvent may be 1-methylnaphthalene, which has a boiling point of about 242° C. at ambient pressure, and suitably this gives sufficient difference in respective boiling points to achieve 100% furfural purity.

Suitably, the distillation step may be a vacuum distillation step. Suitably, the vacuum column may be operated down to a pressure of around 0.00133 MPa (10 mmHg) to lower the boiling point of furfural from about 161° C. Suitably, under such conditions, a top stream comprising furfural, and a bottom stream comprising the aromatic solvent are obtained. Advantageously, the vacuum distillation step overcomes the possibility of furfural loss from heat-induced degradation and oligomerisation.

Suitably, the distillation step may be an atmospheric distillation step, where suitably, furfural can be obtained as the top stream in the region of the distillation column at a temperature of about 160° C. to about 180° C., leaving a bottom stream comprising the aromatic solvent.

Suitably, although the aromatic solvent has a preferred selectivity towards furfural, during the first liquid-liquid separation step, a portion of the furfural may nevertheless remain in the aqueous phase of the composition. The amount of furfural present in the aqueous phase may depend on which aromatic solvent is used, however it may be up to about 60% of the amount of furfural that is present in the composition. This is undesirable, as it may lead to furfural loss, for example, due to degradation and/or oligomerisation of the furfural remaining in the aqueous phase by reacting with other components present in the aqueous phase. It is further undesirable as furfural remaining the aqueous phase forms an azeotrope with water. This complicates the separation of furfural from aqueous phase because the boiling point of the furfural-water azeotrope at ambient pressure is about 98° C., this being very close to the boiling point of water from which it needs to be separated from.

Following the first liquid-liquid separation step, in order to achieve both high furfural recovery and high furfural purity, furfural needs to be recovered efficiently from both the first organic phase (comprising the aromatic solvent and a portion of the furfural) and from the first aqueous phase (comprising the remainder of the furfural and the at least one acid). Further, furfural has to be extracted efficiently from the furfural-water azeotrope.

Therefore, to achieve overall high furfural recovery, high furfural purity and energy efficiency, the inventors have introduced a furfural-water azeotrope enrichment section into the process of the present invention, which efficiently increases extraction of furfural, particularly from the furfural-water azeotrope.

To achieve this, firstly, the water content of the aqueous phase from the first liquid-liquid separation step is reduced by a first distillation step. Secondly, said furfural-water azeotrope stream from the first distillation step is supplied to a second liquid-liquid separator, primarily to reduce the energy consumption of the process by taking advantage of the phase separation property of the furfural-water azeotrope under certain temperatures. Thirdly, following the second liquid-liquid separation step, furfural-water azeotrope enrichment may be carried out by returning a furfural-water azeotrope enriched stream back to the second liquid-liquid separator.

Therefore in the process of the present invention, the aqueous phase (8) is subjected to a first distillation step (15) to provide: (i) a first top stream (13) comprising a furfural-water azeotrope, and (ii) an aqueous waste stream (5) comprising water and the at least one acid.

Suitably, the first distillation step is carried out under mild conditions, such that a top stream of the furfural-water azeotrope is obtained at a temperature of about 98° C.

In the process of the present invention, the first top stream (13) provided by the first distillation step (15) is then subjected to a second liquid-liquid separation step (16) to provide: (i) a second top stream (12) comprising a portion of the furfural-water azeotrope, and (ii) a second bottom stream (10) comprising the remainder of the furfural-water azeotrope.

Preferably, the second liquid-liquid separation may be operated at a temperature of at most 120° C., more preferably at a temperature of at most 100° C., even more preferably at a temperature of at most 80° C., even more preferably at a temperature of at most 60° C., so long as the liquid separates into two phases at the separation temperature.

Preferably, the second liquid-liquid separation may be operated at a temperature of at least ambient temperature, more preferably at a temperature of at least 30° C., even more preferably at a temperature of at least 40° C., even more preferably at a temperature of at least 50° C., so long as the liquid separates into two phases at the separation temperature.

Following the second liquid-liquid separation step, a furfural stream can be obtained from the second top stream by subjecting it to a second distillation step by using the difference in the boiling point of furfural and the furfural-water azeotrope (about 161° C. compared to about 98° C. respectively at ambient pressure). Therefore in the process of the present invention, the second top stream (12) from the second liquid-liquid separation step (16) is subjected to a second distillation step (17) to provide: (i) a third top stream (11) enriched with the furfural-water azeotropic mixture, and (ii) a third bottom stream (4) comprising furfural.

The inventors have also sought to maximise furfural yield by expending low energy, by seeking to enrich furfural levels in the second bottom stream (provided by the second liquid-liquid separation step) via distillation at mild conditions.

Optionally, in an embodiment of the invention, the second bottom stream (10) is subjected to a fourth distillation step (18) to provide: (i) a fifth top stream (9) comprising the furfural-water azeotrope, and a fifth bottom stream (6) comprising water, thereby reducing the water content of the fifth top stream (9), which is recycled back to feed the second liquid-liquid separation step (16). Suitably, the fifth top stream is obtained at a temperature of about 98° C.

For further efficiency and to increase the utility of the aromatic solvent, optionally, the fourth bottom stream (3) from the third distillation step (19) comprising the aromatic solvent is recycled into the composition.

Optionally, in another embodiment of the present invention, the third top stream (11) provided by the second distillation step (17) may be recycled back to feed the second liquid-liquid separation step (16), or the first distillation step (15), or the first liquid-liquid separation step (14).

Optionally, in another embodiment of the present invention, the second bottom stream comprising the remainder of the furfural-water azeotrope provided by the second liquid-liquid separation step (c) is recycled back to feed either the first distillation step of step (b), or the first liquid-liquid separation step of step (a).

Optionally, in a further embodiment of the present invention the aqueous phase provided by the first liquid-liquid separation step (a) is recycled to feed is recycled to the pentose dehydration step.

Optionally, each of the first distillation step, the second distillation step and the third distillation step may be either atmospheric distillation, and vacuum distillation, where if the latter the vacuum column may be operated at a pressure down to around 0.00133 MPa (10 mmHg).

Optionally, each of the first distillation step, the second distillation step, the third distillation and fourth distillation step may be either atmospheric distillation, and vacuum distillation, where if the latter the vacuum column may be operated at a pressure down to around 0.00133 MPa (10 mmHg).

EXAMPLE

A process line up, as depicted in FIG. 1, was assessed for furfural recovery using process modelling Aspen plus (Version 7.3) software licensed from Aspen Technology Inc., MA.

The modelled process line up is representative of a furfural separation scheme from a process stream containing furfural on a furfural manufacturing plant.

The results obtained in this example are representative of expected furfural recovery rates, fraction of furfural recovery from feed stream, furfural purity, heat duty (MW), and steam usage measured in tonne of steam/tonne of furfural produced.

Thermodynamic data contained in ‘NRTL-HOC property method’ set was used in this simulation.

Steam consumption in the process line up was determined on the basis of using 4.48 MPa high pressure steam.

The feed stream (1) contains water, furfural, acetic acid (as at least one organic acid), and 1-methyl naphthalene (1-MNP) (representative of an aromatic solvent with a boiling point higher than that of furfural).

The separation scheme enables separation of furfural from the composition with high purity and allows for recycling of the solvent for re-use in the process. Table 1 presents the process stream data output.

Tables 2 and 3 give process operating conditions and a results summary for distillation columns and liquid-liquid separators used in the process line-up.

Table 4 presents the summary of results for the furfural separation scheme.

Based on the simulation output this separation process line up consumes about 7.6 tonne steam/tonne furfural produced. This is about 24% reduction in steam usage compared to consumption of 10 tonne steam/tonne furfural produced in the state-of-the-art Rosenlew's process for commercial furfural production.

TABLE 1 Stream Summary Results Component Stream # Mass Flow 12 10 9 6 13 5 3 2 11 4 1 7 8 Water 14 519 134 385 385 13980 0 0 14 0 14365 0 14365 (tonnes/day) Furfural 157 66 66 0 146 31 0 454 12 146 631 454 177 (tonnes/day) Acetic Acid 0 0 0 0 0 240 0 0 0 0 240 0 240 (tonnes/day) 1-MNP 0 0 0 0 0 0 7182 0 0 0 7182 7182 0 (tonnes/day) Mass Flow 172 585 200 385 531 14251 7182 455 26 146 22418 7636 14782 Temperature 90 90 97 100 98 100 244 161 97 161 140 140 140 (° C.)

TABLE 2 Distillation Column Summary Units D1 D2 D3 D4 Pressure MPa 0.1 0.1 0.1 0.1 Reflux Ratio 0.7 1 1 1 Distillate Rate tonne/day 531 26 454.5 200 Number of trays 25 25 25 25 Feed rate tonne/day 14782 172 7636 585 Reboiler C. 100 161 244 100 Temperature Reboiler Duty MW 57 1 23 8 Steam usage (4.48 MPa) tonne/day 2924 51 1197 401

TABLE 3 Liquid-Liquid Separator Summary Units LL1 LL2 Pressure MPa 0.1 0.1 Temperature C. 140 90 Feed rate tonne/day 22418 757

TABLE 4 Separation Scheme Results Summary Units Furfural Recovery Rate tonne/day 600.0 Furfural Recovery 95.1% Furfural Purity  100% Total energy requirement MW 89 Steam Usage (650 psig) tonne/day 4573 Steam Consumption t/t FUR produced 7.6 

That which is claimed is:
 1. A process for the extraction of furfural from a composition comprising furfural, water, at least one acid and an aromatic solvent with a boiling point higher than that of furfural; said process comprising: (a) subjecting the composition to a first liquid-liquid separation step to provide: an organic phase comprising the aromatic solvent and a portion of the furfural, and an aqueous phase comprising the remainder of the furfural and the at least one acid; (b) subjecting the aqueous phase of step (a) to a first distillation step to provide: a first top stream comprising a furfural-water azeotrope, and an aqueous waste stream comprising water and the at least one acid; (c) subjecting the first top stream of step (b) to a second liquid-liquid separation step to provide: a second top stream comprising a portion of the furfural-water azeotrope, and a second bottom stream comprising the remainder of the furfural-water azeotrope; (d) subjecting the second top stream of step (c) to a second distillation step to provide: a third top stream enriched with the furfural-water azeotropic mixture, and a third bottom stream comprising furfural; (e) subjecting the organic phase of step (a) to a third distillation step to provide: a fourth bottom stream comprising the aromatic solvent, and a fourth top stream comprising furfural, (f) subjecting the second bottom stream of step (c) to a fourth distillation step to provide: a fifth top stream comprising the furfural-water azeotrope, which is recycled back to feed the second liquid-liquid separation step of step (c), and a fifth bottom stream comprising water.
 2. The process according to claim 1, wherein the composition is derived from a product stream of a pentose dehydration step wherein a pentose feed stream is dehydrated.
 3. The process according to claim 2, wherein the pentose feed stream is derived from the hydrolysis of a lignocellulosic biomass.
 4. The process according to claim 1, wherein the aromatic solvent is selected from the group consisting of 1-ethyl-2,3-dimethylbenzene, 1-ethyl-2,5-dimethylbenzene, 1-ethyl-2,4-dimethylbenzene, 1-ethyl-3,4-dimethylbenzene, 1,2,3,5-tetramethylbenzene, 1,2,3,4-tetramethylbenzene, 1,2,4,5-tetramethylbenzene, naphthalene, 1-methylnaphthalene, 2-methylnaphthalene, n- and sec-propyl-methyl benzenes with the methyl group located in 2-,3-,4- or 5-position, n- and sec-butyl benzene and n- and sec-pentyl benzene, or any combination thereof.
 5. The process according to claim 1, wherein the aromatic solvent has a ratio of aromatic carbons to aliphatic carbons of greater than
 1. 6. The process according to claim 1, wherein the second liquid-liquid separation step is operated at a temperature range of from ambient temperature to 120° C.
 7. The process according to claim 1, wherein the distillation step is an atmospheric distillation step or a vacuum distillation step.
 8. The process according to claim 1, wherein the third top stream of step (d) is recycled back to feed either: the second liquid-liquid separation step of step (c) above, or the first distillation step of step (b), or the first liquid-liquid separation step of step (a). 